CN106166432A - Iodine retracting device and recovery method thereof in a kind of Wet-process Phosphoric Acid Production tail gas - Google Patents
Iodine retracting device and recovery method thereof in a kind of Wet-process Phosphoric Acid Production tail gas Download PDFInfo
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- CN106166432A CN106166432A CN201610779316.4A CN201610779316A CN106166432A CN 106166432 A CN106166432 A CN 106166432A CN 201610779316 A CN201610779316 A CN 201610779316A CN 106166432 A CN106166432 A CN 106166432A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1418—Recovery of products
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—Regeneration of liquid absorbents
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B7/00—Halogens; Halogen acids
- C01B7/13—Iodine; Hydrogen iodide
- C01B7/14—Iodine
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Abstract
The present invention relates to phosphoric acid by wet process tail gas disposal technique field, iodine retracting device and recovery method thereof in especially a kind of Wet-process Phosphoric Acid Production tail gas, by tail gas is carried out absorptive unit a, absorptive unit b, absorptive unit c, after absorptive unit d processes, exhaust temperature can be effectively reduced, make in the silicate fluoride solution of the formation after iodine composition is dissolved in tail gas absorption in a large number in tail gas, and it is capable of cyclic absorption to process, the resources such as the fluorine silicon emptying in tail gas are reclaimed in a large number, but also reduce and avoid iodine discharge, and the process in conjunction with iodine recovery unit, iodine resource is recycled, reduce environmental pollution, improve added value of product in Wet-process Phosphoric Acid Production tail gas, reduce cost.
Description
Technical field
The present invention relates to phosphoric acid by wet process tail gas disposal technique field, in especially a kind of Wet-process Phosphoric Acid Production tail gas, iodine reclaims
Device and recovery method thereof.
Background technology
Iodine is the base stock manufacturing organic and inorganic iodide, is again human body and the requisite nutrient of plant,
The aspect such as medicine, agricultural, dyestuff, metallurgy, rubber, national defence has purposes widely；The iodine main source of China is that sea water extracts
Iodine so that raw material is rare, causes iodine deficiency serious, it is difficult to meet the demand of domestic market.
In addition to containing iodine in the seawater, the rock phosphate in powder on the ground such as Guizhou, Yunnan also contains the oxide of iodine, and
Iodine amount of storage is relatively big, and grade is low, and average amount of iodine is at 19-76mg/kg.During Wet-process Phosphoric Acid Production, the iodine resource in phosphorus ore,
A part enters in tail gas with the form of iodine, because exhaust temperature is about 80 DEG C, and in washing process, generally uses work
Skill water washs, and causes iodine dissolubility in washing absorption liquid relatively low so that iodine along with exhaust emissions in atmosphere, makes
Tail gas must be caused to occur emitting red cigarette phenomenon, and cause the waste of iodine resource.
In prior art, the research for the iodine recovery technology in Wet-process Phosphoric Acid Production tail gas is more, but it is still led
The response rate causing iodine is relatively low, and cost recovery is higher, and by independent with iodine retracting device for exhaust gas processing device so that
While iodine reclaims, it is difficult to phosphoric acid by wet process tail gas is processed, causes and the resource in Wet-process Phosphoric Acid Production tail gas is combined
Close the relatively costly of utilization.
Summary of the invention
In order to solve above-mentioned technical problem present in prior art, the present invention provides in a kind of Wet-process Phosphoric Acid Production tail gas
Iodine retracting device and recovery method thereof.
It is achieved particular by techniques below scheme:
Iodine retracting device in a kind of Wet-process Phosphoric Acid Production tail gas, by iodine recovery unit, absorptive unit a, absorptive unit b, suction
Receive unit c, absorptive unit d composition；Iodine recovery unit is connected with absorptive unit a by pipe a；Absorptive unit a and absorptive unit b leads to
Cross pipe b to connect with pipe c；Absorptive unit b and absorptive unit c is connected by pipe d and pipe e；Absorptive unit c passes through with absorptive unit d
Pipe f connects with pipe g.
Described pipe a is to be sent in iodine recovery unit by the serosity in absorptive unit a；Pipe b be by absorptive unit a not
Absorbing tail gas completely to send in absorptive unit b, pipe c is by the slurry reflux in absorptive unit b to absorptive unit a；Pipe d is
Sending into not absorbing tail gas completely in absorptive unit b in absorptive unit c, pipe e is to inhaling by the slurry reflux in absorptive unit c
Receive in unit b；Pipe f is to send into not absorbing tail gas completely in absorptive unit c in absorptive unit d, and pipe g is by absorptive unit d
In slurry reflux in absorptive unit c.
Described iodine recovery unit includes the oxidation trough connected with pipe a, and the oxidant groove a being connected with oxidation trough, with oxidation
Pump a, pump a that groove connects are connected with shower nozzle in extraction tower, be provided with air intake, arrange outlet bottom extraction tower in the middle part of extraction tower
Being connected with pump b, pump b is connected with villiaumite workshop；Extraction tower top is connected with the sidewall of reduction cell；With reduction liquid bath bottom reduction cell
Connecting, reduction liquid bath is connected with pump c, and pump c is connected with the top of reduction cell and defluorinate groove by tee T；The defluorinate groove end on the lower
Portion's sidewall is connected with pump e, and pump e is connected with villiaumite workshop；Defluorinate groove top is also connected with defluorinating agent groove；Defluorinate groove is near top side
Wall is connected with oxidation trough top, and oxidation trough top is connected with oxidant groove b, and oxidant groove is connected with pump d near bottom sidewall, pump
D is connected with purifying groove top, purifies groove top and is connected with sulfuric acid tank.
Described absorptive unit a includes a fluorine tower, is arranged on the offgas outlet a on a fluorine tower, spray unit a, spray list
Unit b, refluxing opening a, circulation port a, circulation port b, gas inlet a, sulfur dioxide entrance, balance port a, liquid outlet；Wherein circulation port
A, circulation port b are connected by pipeline, and after pooling a pipeline, are connected with pump f, pump g, and pump f and spray unit a is even
Connecing, pump g is connected with spray unit b；Refluxing opening a is connected with pipe c；Offgas outlet a is connected with pipe b；Sulfur dioxide entrance and dioxy
Changing sulfur groove to connect, gas inlet a is connected with tail gas groove；Subsider, subsider is provided with balance port b, balance port b and balance port
A is connected by pipeline, the serosity in equilibrium sedimentation groove and a fluorine tower；It is additionally provided with liquid inlet, purified liquor outlet on subsider, enters liquid
Mouth connects with liquid outlet；Purified liquor outlet is connected with pump h, and pump h is connected with pipe a.
Described absorptive unit b, including difluoro tower, the offgas outlet b being arranged on difluoro tower, offgas outlet b are with pipe d even
Connect；The spray unit c that is arranged on difluoro tower, spray unit d, gas inlet b, refluxing opening b, circulation port c, circulation port d, Hui Xun
Mouth a, refluxing opening c；Wherein refluxing opening c is connected with pipe c, and refluxing opening b is connected with pipe e, and circulation port c and circulation port d pools one
After pipeline, being connected with pump i, pump j, pump i is connected with spray unit c, and pump j is connected with spray unit d；Return and follow mouthful a and be connected with pump k,
Pump k follows a mouthful b be connected with arranging back on Venturi scrubber, and gas inlet b is connected with venturi outlet, venturi inlet and pipe b
Connect.
Described absorptive unit c, including trifluoro tower, the offgas outlet c being arranged on trifluoro tower, spray unit e, spray are single
Unit f, spray unit g, gas inlet c, refluxing opening d, refluxing opening e circulation port e, circulation port f, wherein circulation port e and circulation port f converges
Being connected with pump l, pump m, pump n after being polymerized to a pipeline, pump l is connected with spray unit e, and pump m is connected with spray unit f, pump n and spray
Drench unit g to connect；Refluxing opening d is connected with pipe g, and refluxing opening e is connected with pipe e, and gas inlet c is connected with pipe d, offgas outlet c with
Pipe f connects.
Described absorptive unit d, including tail gas washing tower, the spray unit h being arranged on tail gas washing tower, spray unit
I, spray unit j, gas inlet d, refluxing opening f, slag field water inlet, circulation port g, evacuation port；Circulation port g and pump o, pump p, pump q
Connecting, pump o is connected with spray unit i, pump p is connected with spray unit h, pump q is connected with spray unit j, and refluxing opening f and pipe g is even
Connect；Slag field water inlet is connected with slag field tank；Gas inlet d is connected with pump r, and pump r is connected with demister top, and demister sets
Being equipped with gas inlet e, leakage mouth, spray unit k, leakage mouth is connected with liquid seal trough entrance, and liquid seal trough outlet is connected with pump s, pump s
It is connected with spray unit k, liquid seal trough is provided with fluid infusion mouth, fluid infusion mouth is connected with slag field tank；Gas inlet e and pipe f is even
Connect.
A kind of Wet-process Phosphoric Acid Production washing tail gas absorption plant, by absorptive unit a, absorptive unit b, absorptive unit c, absorption
Unit d forms；Absorptive unit a and absorptive unit b is connected by pipe b and pipe c；Absorptive unit b and absorptive unit c by pipe d and
Pipe e connects；Absorptive unit c and absorptive unit d is connected by pipe f and pipe g；Pipe b is will not absorb tail completely in absorptive unit a
Pneumatic transmission enters in absorptive unit b, and pipe c is by the slurry reflux in absorptive unit b to absorptive unit a；Pipe d is by absorptive unit b
In do not absorb tail gas completely and send in absorptive unit c, pipe e is by the slurry reflux in absorptive unit c to absorptive unit b；
Pipe f is to send into not absorbing tail gas completely in absorptive unit c in absorptive unit d, and pipe g is to be returned by the serosity in absorptive unit d
It flow in absorptive unit c.
A kind of Wet-process Phosphoric Acid Production washing tail gas absorption process, enters the tail gas produced during Wet-process Phosphoric Acid Production
Enter in absorptive unit a after cyclic absorption processes so that tail gas is entered in absorptive unit b by pipe b, warp in absorptive unit b
After crossing cyclic absorption so that tail gas is entered in absorptive unit c by pipe d, in absorptive unit c after cyclic absorption so that tail
Gas is entered in absorptive unit d by pipe f, after level Four cyclic absorption processes so that tail gas empties；And in absorptive unit d
Absorbing serosity and enter in absorptive unit c by pipe g, the absorption serosity in absorptive unit c enters in absorptive unit b by pipe e, inhales
Serosity in receipts unit b is in pipe c enters absorptive unit a, and the recovery reaching to realize loop slurry is collected, and to absorbing slurry
Liquid is circulated process tail gas so that improves the treatment effeciency of tail gas, and enables to tail gas at washing absorption step by step
During, reduce temperature, improve elemental iodine dissolubility in fluosilicate, it is to avoid iodine, along with exhaust emissions, improves
The recovery of resource.
Iodine recovery method in a kind of Wet-process Phosphoric Acid Production tail gas, in above-mentioned washing tail gas absorption process, by absorbing
After serosity is collected in absorptive unit a, in unit a to be absorbed in absorption serosity after mass concentration >=10% of hexafluosilicic acid, pass through
Pipe a enters in iodine recovery unit, and settles in subsider, using the material that sinks as the raw material in white carbon workshop, by supernatant
Liquid delivers to oxidation trough, adds the hydrogen peroxide solution of theoretical amount 120%, reacts 30min, then be passed to extraction at temperature is 70 DEG C
Taking tower, use air as extractant, controlling gas liquid ratio in extraction tower is 100:1, and remaining for extraction liquid is sent to villiaumite workshop, contains
The air of iodine enters reduction hand washing tank, adds the reduction of sulfur dioxide liquid, obtains containing in Reducing and absorption liquid, and absorbing liquid to be restored
After the concentration of I reaches 50g/L, it is passed to defluorinate tower, adds defluorinating agent, after defluorinate processes, deliver to oxidation trough, add
The hydrogen peroxide solution of theoretical amount 120%, is 40 DEG C in temperature, reacts 30min, delivers to the iodine liquid of bottom land purify groove, and mother solution returns
Return oxidation trough；Adding concentrated sulphuric acid in groove to purifying, controlling temperature is 150 DEG C so that iodine natural subsidence, treats that precipitum is not further added by
After, filter, obtain essence iodine.
Compared with prior art, the technique effect of the present invention is embodied in:
By tail gas being carried out absorptive unit a, after absorptive unit b, absorptive unit c, absorptive unit d process, it is possible to
Effectively reduce exhaust temperature so that the silicate fluoride solution of the formation after iodine composition is dissolved in tail gas absorption in a large number in tail gas
In, and it being capable of cyclic absorption process so that the resources such as the fluorine silicon in emptying tail gas are reclaimed in a large number, but also reduce
Avoid iodine discharge, and combine the process of iodine recovery unit so that iodine resource recycled, reduce environment dirt
Dye, improves added value of product in Wet-process Phosphoric Acid Production tail gas, reduces cost.
Accompanying drawing explanation
Fig. 1 is the annexation schematic diagram of apparatus of the present invention.
Fig. 2 is the structural relation figure of in Fig. 11.
Fig. 3 is the structural relation figure of in Fig. 12.
Fig. 4 is the structural relation figure of in Fig. 13.
Fig. 5 is the structural relation figure of in Fig. 14.
Fig. 6 is the structural relation figure of in Fig. 15.
Fig. 7 is the concrete structure schematic diagram of apparatus of the present invention.
1-iodine recovery unit 2-absorptive unit a 3-absorptive unit b 4-absorptive unit c 5-absorptive unit d 6-pipe a 7-
Pipe b 8-pipe c 9-pipe d 10-pipe e 11-pipe f 12-pipe g；
1.1-oxidant groove a 1.2-oxidation trough 1.3-pump a 1.4-extraction tower 1.5-air intake 1.6-pump b 1.7-
Air compressor 1.8-pump c 1.9-reduces liquid bath 1.10-shower nozzle 1.11-reduction cell 1.12-defluorinate groove 1.13-defluorinating agent
Groove 1.14-oxidant groove b 1.15-sulfuric acid tank 1.16-oxidation trough 1.17-pump d 1.18-purifies groove 1.19-pump e；
2.1-mono-fluorine tower 2.2-offgas outlet a 2.3-spray unit a 2.4-spray unit b 2.5-pump f 2.6-pump g
2.7-refluxing opening a 2.8-circulation port a 2.9-circulation port b 2.10-gas inlet a 2.11-sulfur dioxide entrance 2.12-bis-
Sulfur oxide groove 2.13-tail gas groove 2.14-balance port a 2.15-balance port b 2.16-liquid outlet 2.17-liquid inlet 2.18-
Subsider 2.19-pump h 2.20-purified liquor outlet；
3.1-difluoro tower 3.2 offgas outlet b 3.3-spray unit c 3.4-spray unit d 3.5-gas inlet b
3.6-refluxing opening b 3.7-pump i 3.8-pump j 3.9-circulation port c 3.10-circulation port d 3.11-returns and follows a mouthful a 3.12-pump k
3.13-refluxing opening c 3.14-venturi outlet 3.15-returns and follows a mouthful b 3.16-venturi inlet 3.17-Venturi scrubber；
4.1-trifluoro tower 4.2-offgas outlet c 4.3-spray unit e 4.4-spray unit f 4.5-spray unit g
4.6-gas inlet c 4.7-refluxing opening d 4.8-refluxing opening e 4.9-circulation port e 4.10-circulation port f 4.11-pump l 4.12-
Pump m 4.13-pump n；
5.1-tail gas washing tower 5.2-spray unit h 5.3-spray unit i 5.4-spray unit j 5.5-pump o 5.6-
Water inlet 5.11-gas inlet d 5.12-slag field, pump p 5.7-pump q 5.8-circulation port g 5.9-refluxing opening f 5.10-slag field
Tank 5.13-pump r 5.14-pump s 5.15-spray unit k 5.16-demister 5.17-gas inlet e 5.18-leakage mouth
5.19-liquid seal trough entrance 5.20-fluid infusion mouth 5.21-liquid seal trough exports.
Detailed description of the invention
With specific embodiment, technical scheme is further limited below in conjunction with the accompanying drawings, but requirement
The scope of protection is not only limited to description.
Embodiment
As it is shown in figure 1, iodine retracting device in a kind of Wet-process Phosphoric Acid Production tail gas, by iodine recovery unit 1, absorptive unit a2,
Absorptive unit b3, absorptive unit c4, absorptive unit d5 form；Iodine recovery unit 1 is connected with absorptive unit a2 by pipe a6；Absorb
Unit a2 and absorptive unit b3 is connected by pipe b7 and pipe c8；Absorptive unit b3 and absorptive unit c4 is by pipe d9 and pipe e10 even
Logical；Absorptive unit c4 and absorptive unit d5 is connected by pipe f11 and pipe g12.
Described pipe a6 is to be sent in iodine recovery unit 1 by the serosity in absorptive unit a2；Pipe b7 is by absorptive unit
Not absorbing tail gas completely in a2 to send in absorptive unit b3, pipe c8 is to absorptive unit by the slurry reflux in absorptive unit b3
In a2；Pipe d9 is to send into not absorbing tail gas completely in absorptive unit b3 in absorptive unit c4, and pipe e10 is by absorptive unit c4
In slurry reflux in absorptive unit b3；Pipe f11 is to send not absorbing tail gas completely in absorptive unit c4 into absorptive unit
In d5, pipe g12 is by the slurry reflux in absorptive unit d5 to absorptive unit c4.
As shown in Figure 1 and Figure 2, in certain embodiments, described iodine recovery unit 1 includes the oxidation trough connected with pipe a6
In 1.2, the oxidant groove a1.1 being connected with oxidation trough 1.2, the pump a1.3 being connected with oxidation trough 1.2, pump a1.3 and extraction tower 1.4
Shower nozzle 1.10 connects, and is provided with air intake 1.5 in the middle part of extraction tower 1.4, arranges outlet with pump b1.6 even bottom extraction tower 1.4
Connecing, pump b1.6 is connected with villiaumite workshop；Extraction tower 1.4 top is connected with the sidewall of reduction cell 1.11；Bottom reduction cell 1.11 with
Reduction liquid bath 1.9 connects, and reduction liquid bath 1.9 is connected with pump c1.8, and pump c1.8 is by tee T and reduction cell 1.11 and defluorinate groove
The top of 1.12 connects；Defluorinate groove 1.12 bottom sidewall on the lower is connected with pump e1.19, and pump e1.19 is connected with villiaumite workshop；De-
Fluorine groove 1.12 top is also connected with defluorinating agent groove 1.13；Defluorinate groove 1.12 is connected with oxidation trough 1.16 top near top sidewall,
Oxidation trough 1.16 top is connected with oxidant groove b1.14, and oxidant groove 1.16 is connected with pump d1.17 near bottom sidewall, pump
D1.17 is connected with purifying groove 1.18 top, purifies groove 1.18 top and is connected with sulfuric acid tank 1.15.
As shown in Figure 1, Figure 3, in certain embodiments, described absorptive unit a2 includes a fluorine tower 2.1, is arranged on a fluorine
Offgas outlet a2.2 on tower 2.1, spray unit a2.3, spray unit b2.4, refluxing opening a2.7, circulation port a2.8, circulation port
B2.9, gas inlet a2.10, sulfur dioxide entrance 2.11, balance port a2.14, liquid outlet 2.16；Wherein circulation port a2.8, follow
Collar extension b2.9 is connected by pipeline, and after pooling a pipeline, is connected with pump f2.5, pump g2.6, and pump f2.5 and spray
Unit a2.3 connects, and pump g2.6 is connected with spray unit b；Refluxing opening a2.7 is connected with pipe c8；Offgas outlet a2.2 and pipe b7 is even
Connect；Sulfur dioxide entrance 2.11 is connected with sulfur dioxide groove 2.12, and gas inlet a2.10 is connected with tail gas groove 2.13；Subsider
2.18, subsider 2.18 is provided with balance port b2.15, balance port b2.15 is connected by pipeline with balance port a2.14, balance
Serosity in subsider 2.18 and a fluorine tower 2.1；It is additionally provided with liquid inlet 2.17, purified liquor outlet 2.20 on subsider 2.18, enters
Liquid mouth 2.17 connects with liquid outlet 2.16；Purified liquor outlet 2.20 is connected with pump h2.19, and pump h2.19 is connected with pipe a6.
As Figure 1 and Figure 4, in certain embodiments, described absorptive unit b3, including difluoro tower 3.1, it is arranged on two
Offgas outlet b3.2 on fluorine tower 3.1, offgas outlet b3.2 are connected with pipe d9；It is arranged on the spray unit on difluoro tower 3.1
C3.3, spray unit d3.4, gas inlet b3.5, refluxing opening b3.6, circulation port c3.9, circulation port d3.10, return follow a mouthful a3.11,
Refluxing opening c3.13；Wherein refluxing opening c3.13 is connected with pipe c8, and refluxing opening b3.6 is connected with pipe e10, circulation port c3.9 and circulation
After mouthful d3.10 pools a pipeline, being connected with pump i3.7, pump j3.8, pump i3.7 is connected with spray unit c3.3, pump j3.8 and
Spray unit d3.4 connects；Return and follow mouthful a3.11 and be connected with pump k3.12, pump k3.12 and Venturi scrubber 3.17 arrange Hui Xun
Mouth b3.15 connects, and gas inlet b3.5 is connected with venturi outlet 3.14, and venturi inlet is connected with pipe b7.
As shown in Figure 1, shown in Figure 5, in certain embodiments, described absorptive unit c4, including trifluoro tower 4.1, it is arranged on three
Offgas outlet c4.2 on fluorine tower 4.1, spray unit e4.3, spray unit f4.4, spray unit g4.5, gas inlet c4.6,
Refluxing opening d4.7, refluxing opening e4.8 circulation port e4.9, circulation port f4.10, wherein circulation port e4.9 pools with circulation port f4.10
Being connected with pump l4.11, pump m4.12, pump n4.13 after a piece pipeline, pump l4.11 is connected with spray unit e4.3, pump m4.12 and spray
Drenching unit f4.4 to connect, pump n4.13 is connected with spray unit g4.5；Refluxing opening d4.7 is connected with pipe g12, refluxing opening e4.8 and pipe
E10 connects, and gas inlet c4.6 is connected with pipe d9, and offgas outlet c4.2 is connected with pipe f11.
As shown in Fig. 1, Fig. 6, in certain embodiments, described absorptive unit d5, including tail gas washing tower 5.1, arrange
Spray unit h5.2 on tail gas washing tower 5.1, spray unit i5.3, spray unit j5.4, gas inlet d5.11, backflow
Mouth f5.9, slag field water inlet 5.10, circulation port g5.8, evacuation port；Circulation port g5.8 and pump o5.5, pump p5.6, pump q5.7 are connected,
Pump o5.5 is connected with spray unit i5.3, pump p5.6 is connected with spray unit h5.2, pump q5.7 is connected with spray unit j5.4, returns
Head piece f5.9 is connected with pipe g12；Slag field water inlet 5.10 is connected with slag field tank 5.12；Gas inlet d5.11 and pump r5.13 is even
Connecing, pump r5.13 is connected with demister 5.16 top, and demister 5.16 is provided with gas inlet e5.17, leakage mouth 5.18, spray
Drenching unit k5.15, leakage mouth 5.18 is connected with liquid seal trough entrance 5.19, and liquid seal trough outlet 5.21 is connected with pump s5.14, pump
S5.14 is connected with spray unit k5.15, is provided with fluid infusion mouth 5.20, fluid infusion mouth 5.20 and slag field tank 5.12 on liquid seal trough
Connect；Gas inlet e5.17 is connected with pipe f11.
In certain embodiments, the present invention can also is that a kind of Wet-process Phosphoric Acid Production washing tail gas absorption plant, by absorbing
Unit a2, absorptive unit b3, absorptive unit c4, absorptive unit d5 form；Absorptive unit a2 and absorptive unit b3 by pipe b7 and
Pipe c8 connects；Absorptive unit b3 and absorptive unit c4 is connected by pipe d9 and pipe e10；Absorptive unit c4 passes through with absorptive unit d5
Pipe f11 connects with pipe g12；Pipe b7 is to send into not absorbing tail gas completely in absorptive unit a2 in absorptive unit b3, and pipe c8 is
By in the slurry reflux in absorptive unit b3 to absorptive unit a2；Pipe d9 is to send not absorbing tail gas completely in absorptive unit b3
Entering in absorptive unit c4, pipe e10 is by the slurry reflux in absorptive unit c4 to absorptive unit b3；Pipe f11 is that absorption is single
Not absorbing tail gas completely in unit c4 to send in absorptive unit d5, pipe g12 is to absorbing by the slurry reflux in absorptive unit d5
In unit c4.
In certain embodiments, the method that above-mentioned washing tail gas absorption plant carries out phosphoric acid by wet process washing tail gas absorption is used
It it is that the tail gas that will produce during Wet-process Phosphoric Acid Production enters in absorptive unit a2 after cyclic absorption processes so that tail
Gas is entered in absorptive unit b3 by pipe b7, in absorptive unit b3 after cyclic absorption so that tail gas is entered by pipe d9 and absorbs
In unit c4, in absorptive unit c4 after cyclic absorption so that tail gas is entered in absorptive unit d5 by pipe f11, Jing Guosi
After level cyclic absorption processes so that tail gas empties；And the absorption serosity in absorptive unit d5 enters absorptive unit by pipe g12
In c4, the absorption serosity in absorptive unit c4 enters in absorptive unit b3 by pipe e10, and the serosity in absorptive unit b3 is through pipe
C8 enters in absorptive unit a2, and the recovery reaching to realize loop slurry is collected, and is circulated process tail gas to absorbing serosity,
Treatment effeciency to tail gas is improved, and enables to tail gas during washing absorption step by step, reduce temperature, improve
Elemental iodine dissolubility in fluosilicate, it is to avoid iodine, along with exhaust emissions, improves the recovery of resource.
In certain embodiments, above-mentioned iodine retracting device is used to carry out iodine recovery method in Wet-process Phosphoric Acid Production tail gas,
In above-mentioned washing tail gas absorption process, after absorption serosity is collected in absorptive unit a2, unit a2 to be absorbed inhales
Receive in serosity after mass concentration >=10% of hexafluosilicic acid, entered in iodine recovery unit 1 by pipe a6, and settle in subsider,
Using the material of sinking as the raw material in white carbon workshop, supernatant being delivered to oxidation trough, the dioxygen adding theoretical amount 120% is water-soluble
Liquid, reacts 30min at temperature is 70 DEG C, then is passed to extraction tower, use air as extractant, control gas in extraction tower
Liquor ratio is 100:1, and remaining for extraction liquid is sent to villiaumite workshop, and the air containing iodine enters reduction hand washing tank, adds sulfur dioxide liquid
Body reduces, and after obtaining reaching 50g/L containing the concentration of I in Reducing and absorption liquid, and absorbing liquid to be restored, is passed to defluorinate
Tower, adds defluorinating agent, after defluorinate processes, delivers to oxidation trough, adds the hydrogen peroxide solution of theoretical amount 120%, be 40 DEG C in temperature,
Reaction 30min, delivers to the iodine liquid of bottom land purify groove, and mother solution returns oxidation trough；To purifying, groove adds concentrated sulphuric acid, control temperature
It is 150 DEG C so that iodine natural subsidence, after precipitum is not further added by, filters, obtain essence iodine.
Claims (10)
1. iodine retracting device in a Wet-process Phosphoric Acid Production tail gas, it is characterised in that by iodine recovery unit (1), absorptive unit a
(2), absorptive unit b (3), absorptive unit c (4), absorptive unit d (5) composition；Iodine recovery unit (1) is by pipe a (6) and absorption
Unit a (2) connects；Absorptive unit a (2) and absorptive unit b (3) is connected by pipe b (7) and pipe c (8)；Absorptive unit b (3) with
Absorptive unit c (4) is connected by pipe d (9) and pipe e (10)；Absorptive unit c (4) and absorptive unit d (5) is by pipe f (11) and pipe
G (12) connects.
2. iodine retracting device in Wet-process Phosphoric Acid Production tail gas as claimed in claim 1, it is characterised in that described pipe a (6) is
Serosity in absorptive unit a (2) is sent in iodine recovery unit (1)；Pipe b (7) is will not absorbed in absorptive unit a (2)
Full tail gas is sent in absorptive unit b (3), and pipe c (8) is by the slurry reflux in absorptive unit b (3) to absorptive unit a (2)
In；Pipe d (9) is not absorb during tail gas sends into absorptive unit c (4) completely in absorptive unit b (3), and pipe e (10) is to absorb
Slurry reflux in unit c (4) is in absorptive unit b (3)；Pipe f (11) is will not absorb tail completely in absorptive unit c (4)
Pneumatic transmission enters in absorptive unit d (5), and pipe g (12) is by the slurry reflux in absorptive unit d (5) to absorptive unit c (4).
3. iodine retracting device in Wet-process Phosphoric Acid Production tail gas as claimed in claim 1 or 2, it is characterised in that described iodine returns
Receiving the oxidation trough (1.2) that unit (1) includes connecting with pipe a (6), oxidant groove a (1.1) being connected with oxidation trough (1.2), with oxygen
Pump a (1.3), pump a (1.3) that change groove (1.2) connects are connected with extraction tower (1.4) interior shower nozzle (1.10), extraction tower (1.4) middle part
Being provided with air intake (1.5), extraction tower (1.4) bottom arranges outlet and is connected with pump b (1.6), pump b (1.6) and villiaumite workshop
Connect；Extraction tower (1.4) top is connected with the sidewall of reduction cell (1.11)；Reduction cell (1.11) bottom and reduction liquid bath (1.9)
Connecting, reduction liquid bath (1.9) is connected with pump c (1.8), and pump c (1.8) is by tee T and reduction cell (1.11) and defluorinate groove
(1.12) top connects；Defluorinate groove (1.12) bottom sidewall on the lower is connected with pump e (1.19), pump e (1.19) and villiaumite car
Between connect；Defluorinate groove (1.12) top is also connected with defluorinating agent groove (1.13)；Defluorinate groove (1.12) is near top sidewall and oxidation
Groove (1.16) top connects, and oxidation trough (1.16) top is connected with oxidant groove b (1.14), and oxidant groove (1.16) is near bottom
Sidewall is connected with pump d (1.17), and pump d (1.17) is connected with purifying groove (1.18) top, purifies groove (1.18) top and sulfuric acid tank
(1.15) connect.
4. iodine retracting device in Wet-process Phosphoric Acid Production tail gas as claimed in claim 1 or 2, it is characterised in that described absorption
Unit a (2) includes a fluorine tower (2.1), is arranged on the offgas outlet a (2.2) on a fluorine tower (2.1), spray unit a (2.3), spray
Drench unit b (2.4), refluxing opening a (2.7), circulation port a (2.8), circulation port b (2.9), gas inlet a (2.10), sulfur dioxide
Entrance (2.11), balance port a (2.14), liquid outlet (2.16)；Wherein circulation port a (2.8), circulation port b (2.9) are by pipeline even
Connect, and after pooling a pipeline, be connected with pump f (2.5), pump g (2.6), and pump f (2.5) and spray unit a (2.3) is even
Connecing, pump g (2.6) is connected with spray unit b；Refluxing opening a (2.7) and pipe c (8) is connected；Offgas outlet a (2.2) and pipe b (7) is even
Connect；Sulfur dioxide entrance (2.11) is connected with sulfur dioxide groove (2.12), and gas inlet a (2.10) is with tail gas groove (2.13) even
Connect；Subsider (2.18), subsider (2.18) is provided with balance port b (2.15), balance port b (2.15) and balance port a
(2.14) connected by pipeline, equilibrium sedimentation groove (2.18) and the serosity in a fluorine tower (2.1)；Subsider also sets up on (2.18)
Having liquid inlet (2.17), purified liquor outlet (2.20), liquid inlet (2.17) connects with liquid outlet (2.16)；Purified liquor outlet (2.20) with
Pump h (2.19) connects, and pump h (2.19) and pipe a (6) is connected.
5. iodine retracting device in Wet-process Phosphoric Acid Production tail gas as claimed in claim 1 or 2, it is characterised in that described absorption
Unit b (3), including difluoro tower (3.1), the offgas outlet b (3.2) being arranged on difluoro tower (3.1), offgas outlet b (3.2) with
Pipe d (9) connects；The spray unit c (3.3) that is arranged on difluoro tower (3.1), spray unit d (3.4), gas inlet b (3.5),
Refluxing opening b (3.6), circulation port c (3.9), circulation port d (3.10), return follow a mouthful a (3.11), refluxing opening c (3.13)；Wherein reflux
Mouth c (3.13) is connected with pipe c (8), and refluxing opening b (3.6) and pipe e (10) is connected, and circulation port c (3.9) and circulation port d (3.10) converges
After being polymerized to a pipeline, being connected with pump i (3.7), pump j (3.8), pump i (3.7) and spray unit c (3.3) is connected, pump j (3.8)
It is connected with spray unit d (3.4)；Return and follow a mouthful a (3.11) and pump k (3.12) and be connected, pump k (3.12) and Venturi scrubber
(3.17) upper setting back follows a mouthful b (3.15) connection, and gas inlet b (3.5) is connected with venturi outlet (3.14), venturi inlet
It is connected with pipe b (7).
6. iodine retracting device in Wet-process Phosphoric Acid Production tail gas as claimed in claim 1 or 2, it is characterised in that described absorption
Unit c (4), including trifluoro tower (4.1), the offgas outlet c (4.2) being arranged on trifluoro tower (4.1), spray unit e (4.3),
Spray unit f (4.4), spray unit g (4.5), gas inlet c (4.6), refluxing opening d (4.7), refluxing opening e (4.8) circulation port e
(4.9), circulation port f (4.10), with pump l after wherein circulation port e (4.9) and circulation port f (4.10) pool a pipeline
(4.11), pump m (4.12), pump n (4.13) connect, pump l (4.11) and spray unit e (4.3) is connected, pump m (4.12) and spray
Unit f (4.4) connects, and pump n (4.13) and spray unit g (4.5) is connected；Refluxing opening d (4.7) and pipe g (12) is connected, refluxing opening
E (4.8) and pipe e (10) is connected, and gas inlet c (4.6) and pipe d (9) is connected, and offgas outlet c (4.2) and pipe f (11) is connected.
7. iodine retracting device in Wet-process Phosphoric Acid Production tail gas as claimed in claim 1 or 2, it is characterised in that described absorption
Unit d (5), including tail gas washing tower (5.1), the spray unit h (5.2) being arranged on tail gas washing tower (5.1), spray unit
I (5.3), spray unit j (5.4), gas inlet d (5.11), refluxing opening f (5.9), slag field water inlet (5.10), circulation port g
(5.8), evacuation port；Circulation port g (5.8) and pump o (5.5), pump p (5.6), pump q (5.7) are connected, pump o (5.5) and spray unit i
(5.3) connect, pump p (5.6) and spray unit h (5.2) is connected, pump q (5.7) and spray unit j (5.4) is connected, refluxing opening f
(5.9) it is connected with pipe g (12)；Slag field water inlet (5.10) is connected with slag field tank (5.12)；Gas inlet d (5.11) and pump r
(5.13) connecting, pump r (5.13) is connected with demister (5.16) top, and demister is provided with gas inlet e on (5.16)
(5.17), leakage mouth (5.18), spray unit k (5.15), leakage mouth (5.18) is connected with liquid seal trough entrance (5.19), liquid seal trough
Outlet (5.21) is connected with pump s (5.14), and pump s (5.14) and spray unit k (5.15) is connected, and is provided with fluid infusion on liquid seal trough
Mouth (5.20), fluid infusion mouth (5.20) are connected with slag field tank (5.12)；Gas inlet e (5.17) and pipe f (11) is connected.
8. a Wet-process Phosphoric Acid Production washing tail gas absorption plant, it is characterised in that by absorptive unit a (2), absorptive unit b
(3), absorptive unit c (4), absorptive unit d (5) composition；Absorptive unit a (2) and absorptive unit b (3) is by pipe b (7) and pipe c
(8) connection；Absorptive unit b (3) and absorptive unit c (4) is connected by pipe d (9) and pipe e (10)；Absorptive unit c (4) and absorption
Unit d (5) is connected by pipe f (11) and pipe g (12)；Pipe b (7) is to send into not absorbing tail gas completely in absorptive unit a (2)
In absorptive unit b (3), pipe c (8) is by the slurry reflux in absorptive unit b (3) to absorptive unit a (2)；Pipe d (9) be by
Not absorbing during tail gas sends into absorptive unit c (4) completely in absorptive unit b (3), pipe e (10) is by absorptive unit c (4)
Slurry reflux is in absorptive unit b (3)；Pipe f (11) is to send not absorbing tail gas completely in absorptive unit c (4) into absorption list
In unit d (5), pipe g (12) is by the slurry reflux in absorptive unit d (5) to absorptive unit c (4).
9. a Wet-process Phosphoric Acid Production washing tail gas absorption process, it is characterised in that will produce during Wet-process Phosphoric Acid Production
In raw tail gas entrance absorptive unit a (2) after cyclic absorption processes so that tail gas is entered absorptive unit b (3) by pipe b (7)
In, in absorptive unit b (3) after cyclic absorption so that tail gas is entered in absorptive unit c (4) by pipe d (9), single absorbing
In unit c (4) after cyclic absorption so that tail gas is entered in absorptive unit d (5) by pipe f (11), at level Four cyclic absorption
After reason so that tail gas empties；And the absorption serosity in absorptive unit d (5) enters in absorptive unit c (4) by pipe g (12),
Absorption serosity in absorptive unit c (4) enters in absorptive unit b (3) by pipe e (10), the serosity warp in absorptive unit b (3)
Crossing pipe c (8) to enter in absorptive unit a (2), the recovery reaching to realize loop slurry is collected, and is circulated absorbing serosity
Process tail gas so that the treatment effeciency of tail gas is improved, and enable to tail gas during washing absorption step by step, reduce
Temperature, improves elemental iodine dissolubility in fluosilicate, it is to avoid iodine, along with exhaust emissions, improves the recovery of resource.
10. iodine recovery method in a Wet-process Phosphoric Acid Production tail gas, it is characterised in that the washing tail gas in claim 9 absorbs
In method, after being collected in absorptive unit a (2) by absorption serosity, unit a (2) to be absorbed absorbs hexafluosilicic acid in serosity
Mass concentration >=10% after, entered in iodine recovery unit (1) by pipe a (6), and settle in subsider, the thing that will sink
Expect the raw material as white carbon workshop, supernatant is delivered to oxidation trough, add the hydrogen peroxide solution of theoretical amount 120%, in temperature
Being reaction 30min at 70 DEG C, then be passed to extraction tower, use air as extractant, controlling gas liquid ratio in extraction tower is
100:1, and remaining for extraction liquid is sent to villiaumite workshop, the air containing iodine enters reduction hand washing tank, adds the reduction of sulfur dioxide liquid,
After obtaining Reducing and absorption liquid, and absorbing liquid to be restored reach 50g/L containing the concentration of I, it is passed to defluorinate tower, adds
Defluorinating agent, after defluorinate processes, delivers to oxidation trough, adds the hydrogen peroxide solution of theoretical amount 120%, be 40 DEG C in temperature, reaction
30min, delivers to the iodine liquid of bottom land purify groove, and mother solution returns oxidation trough；Adding concentrated sulphuric acid in groove to purifying, controlling temperature is
150 DEG C so that iodine natural subsidence, after precipitum is not further added by, filter, obtain essence iodine.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610779316.4A CN106166432A (en) | 2016-08-31 | 2016-08-31 | Iodine retracting device and recovery method thereof in a kind of Wet-process Phosphoric Acid Production tail gas |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610779316.4A CN106166432A (en) | 2016-08-31 | 2016-08-31 | Iodine retracting device and recovery method thereof in a kind of Wet-process Phosphoric Acid Production tail gas |
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| CN106166432A true CN106166432A (en) | 2016-11-30 |
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS513394A (en) * | 1974-06-29 | 1976-01-12 | Nippon Oxygen Co Ltd | CHITSUSOSANKABUTSUTO SHOSANMISUTONO JOKYOHOHO |
| CN101318626A (en) * | 2008-07-10 | 2008-12-10 | 贵州大学 | Apparatus for recycling iodine from diluted phosphoric acid for phosphoric acid manufacture with wet-process |
| CN101428191A (en) * | 2008-11-13 | 2009-05-13 | 贵州开磷（集团）有限责任公司 | Method for improving washing efficiency for tail gas from wet-process phosphoric acid manufacture |
| CN104906920A (en) * | 2015-06-03 | 2015-09-16 | 贵州开磷集团股份有限公司 | System for recycling fluorine and silicon resources from wet-process phosphoric acid tail gas and recovery method thereof |
| CN206214989U (en) * | 2016-08-31 | 2017-06-06 | 贵阳开磷化肥有限公司 | Iodine retracting device in a kind of Wet-process Phosphoric Acid Production tail gas |
-
2016
- 2016-08-31 CN CN201610779316.4A patent/CN106166432A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS513394A (en) * | 1974-06-29 | 1976-01-12 | Nippon Oxygen Co Ltd | CHITSUSOSANKABUTSUTO SHOSANMISUTONO JOKYOHOHO |
| CN101318626A (en) * | 2008-07-10 | 2008-12-10 | 贵州大学 | Apparatus for recycling iodine from diluted phosphoric acid for phosphoric acid manufacture with wet-process |
| CN101428191A (en) * | 2008-11-13 | 2009-05-13 | 贵州开磷（集团）有限责任公司 | Method for improving washing efficiency for tail gas from wet-process phosphoric acid manufacture |
| CN104906920A (en) * | 2015-06-03 | 2015-09-16 | 贵州开磷集团股份有限公司 | System for recycling fluorine and silicon resources from wet-process phosphoric acid tail gas and recovery method thereof |
| CN206214989U (en) * | 2016-08-31 | 2017-06-06 | 贵阳开磷化肥有限公司 | Iodine retracting device in a kind of Wet-process Phosphoric Acid Production tail gas |
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